EP0163865B1 - Procédé pour l'extrusion en une seule phase de produits extrudés en matière polymérique réticulés - Google Patents

Procédé pour l'extrusion en une seule phase de produits extrudés en matière polymérique réticulés Download PDF

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Publication number
EP0163865B1
EP0163865B1 EP85104444A EP85104444A EP0163865B1 EP 0163865 B1 EP0163865 B1 EP 0163865B1 EP 85104444 A EP85104444 A EP 85104444A EP 85104444 A EP85104444 A EP 85104444A EP 0163865 B1 EP0163865 B1 EP 0163865B1
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EP
European Patent Office
Prior art keywords
polymer
stator
mixer
rotor
extruder
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
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EP85104444A
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German (de)
English (en)
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EP0163865A1 (fr
Inventor
George M. Gale
Aldo A. Sorio
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Rapra Technology Ltd
Union Carbide Corp
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Rapra Technology Ltd
Union Carbide Corp
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Priority to AT85104444T priority Critical patent/ATE35106T1/de
Priority to IN281/MAS/85A priority patent/IN164638B/en
Publication of EP0163865A1 publication Critical patent/EP0163865A1/fr
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Publication of EP0163865B1 publication Critical patent/EP0163865B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F255/00—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00
    • C08F255/02—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00 on to polymers of olefins having two or three carbon atoms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/375—Plasticisers, homogenisers or feeders comprising two or more stages
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/465—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using rollers
    • B29C48/467—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using rollers using single rollers, e.g. provided with protrusions, closely surrounded by a housing with movement of the material in the axial direction
    • B29C48/468—Cavity transfer mixing devices, i.e. a roller and surrounding barrel both provided with cavities; Barrels and rollers therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/53—Screws having a varying channel depth, e.g. varying the diameter of the longitudinal screw trunk
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L43/00—Compositions of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and containing boron, silicon, phosphorus, selenium, tellurium or a metal; Compositions of derivatives of such polymers
    • C08L43/04—Homopolymers or copolymers of monomers containing silicon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/022—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the choice of material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
    • B29C48/12—Articles with an irregular circumference when viewed in cross-section, e.g. window profiles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/285—Feeding the extrusion material to the extruder
    • B29C48/288—Feeding the extrusion material to the extruder in solid form, e.g. powder or granules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/285—Feeding the extrusion material to the extruder
    • B29C48/29—Feeding the extrusion material to the extruder in liquid form
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2023/00—Use of polyalkenes or derivatives thereof as moulding material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2105/00—Condition, form or state of moulded material or of the material to be shaped
    • B29K2105/0005—Condition, form or state of moulded material or of the material to be shaped containing compounding ingredients
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2105/00—Condition, form or state of moulded material or of the material to be shaped
    • B29K2105/24—Condition, form or state of moulded material or of the material to be shaped crosslinked or vulcanised
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29L—INDEXING SCHEME ASSOCIATED WITH SUBCLASS B29C, RELATING TO PARTICULAR ARTICLES
    • B29L2023/00—Tubular articles

Definitions

  • the present invention relates to methods for producing shaped, crosslinked, extruded polymeric products and more specifically relates to the production of shaped, crosslinked, extruded polyethylene products.
  • Extruders usable in the one-step process are substantially longer at 30:1 length to diameter ratio which is substantially longer than the 20:1 or 24:1 length to diameter of the majority of conventional extruders now in use. Additionally, a special extruder screw design as known from GB-A-964,428 is needed in the one-step process. In this special screw design, the material to be extruded is forced over the flight of the screw from a rapidly-converging blind passage into a very slowly converging passage, followed by a slightly converging zone and thence through a metering zone of uniform cross-section.
  • suitable control of temperature in the extruder of the one-step process is necessary to prevent the high temperature in the metering zone (where grafting is caused to occur at relatively high temperatures of about 230°C more or less) from creeping into the other zones to produce higher temperatures in the other zones which normally operate at about 130°C.
  • the temperature (230°C) used in the metering (grafting) zone of the one-step process is considerably higher than the temperature used in the grafting process of the earlier patents, e.g., 135°C to 140°C in US ⁇ A ⁇ 3,075,948 and 180°C to 200°C in US-A-3,646,155.
  • the one-step process is not readily adaptable to conventional extruders currently operated on production lines and new extruders and associated equipment must be purchased and installed in order to carry out the one-step process or difficult and expensive changes must be made if conventional extruders are converted.
  • Mixers are often employed at the discharge ends of extruders for the purpose of insuring the uniformity of the material being extruded.
  • US ⁇ A ⁇ 4,169,679 and 4,302,409 describe mixer heads adapted to be attached to the discharge ends of an existing extruder forwarding screw by means of screw threads or any other means.
  • the mixer head is disposed in the extruder barrel between the screw and the die and turns with the screw to mix the compacted, molten polymer delivered to it by the forwarding screw.
  • a fluid additive such as a blowing agent, can be introduced through the barrel wall to the molten polymer at the upstream end of the mixer head.
  • US-A-2,540,146 and 3,035,303 illustrate the use of mixing heads constructed on the downstream end of an extruder screw upstream from the extrusion die but fail to disclose or suggest the provision of a mixer head adapted to be attached at the downstream end of an existing extruder or conducting a grafting reaction to produce a crosslinkable polymer composition.
  • Mixer heads which can be adapted to be fitted onto existing extruders are known from US ⁇ A ⁇ 4,419,014 and GB-A-930,339 in which the mixing elements on the facing surfaces of the rotor and stator are cavities. The molten polymer is forced by the forwarding screw through the cavities which apply a shearing, mixing action on the polymer as the rotor turns.
  • GB-A-1,475,216 describes a mixer head that can be adapted to be fitted onto existing extruders in which the mixer head utilized grooves and lands on the facing surfaces of the rotor and stator. None of these patents disclose or suggest the possibility of carrying out the grafting reaction in the mixer head to produce a crosslinkable polymer composition.
  • a plastics extruder known from GB-A-2 059 864 has means for injecting liquid additives such as agents for foaming, colouration or vulcanisation between two mixing sections and of relatively large cross-sectional flow area for the molten plastics, through a plurality of injection nozzles arranged around the circumference of the extruder.
  • liquid additives such as agents for foaming, colouration or vulcanisation between two mixing sections and of relatively large cross-sectional flow area for the molten plastics
  • an extruder mixer for the extrusion of molten plastics and rubbers comprising a hollow cylindrical stator member and a cylindrical rotor member rotatable within the stator.
  • the facing cylindrical surfaces carry rows of hemispherical cavities extending peripherally around the members so that the rows of one member are axially offset from rows of the other member whereby there is an axial overlap of the cavities and rotor.
  • the cavities in adjacent rows on the rotor and stator are also circumferentially offest.
  • a method and a reactor for producing cold-cross-linked polyethylene are known in which a cross-linking agent in the form of a silane and a peroxide catalyst including an organometal compound as cross-linking catalyst are added to the polyethylene to be processed at approximately 100°C, subsequently the polymer is plasticized and the plastification is effected in an extruder. That means that in this known method the plastification of the polymer is effected already in the presence of the cross-linking agent. Said publication does not disclose details as regards the silane to be used.
  • This known method is concerned with preventing possible interferences in the cross-linking by reactions during the plastification of the polymer which are due to an uncontrolled water content in the starting substances. That means that in the known method evaporation of the water content is to take place already in the worm extruder, so that an addition of the cross-linking agent silane+peroxide component at the beginning of the plasticizing process becomes possible.
  • the organometal compound that is in a position to catalyze the silanol condensation is incorporated only into the plasticized premixture. This problem has nothing in common with the problem to be solved by the subject invention.
  • This invention is based on the unexpected discovery that the grafting reaction of a hydrolyzable, olefinically unsaturated silane onto a polymer such as polyethylene can be carried out in a mixing head mounted on and powered by an extruder and to which the polymer, in compacted, melted form, is fed by the extruder. While the compacted, melted polymer is fed to the mixer, compounding ingredients including the silane, a free-radical generator to initiate the grafting reaction in the mixer and, preferably, a silanol condensation catalyst to catalyze the subsequent crosslinking reaction are injected into the compacted, molten polymer just before or just after it is fed into the mixing head.
  • the silanol condensation catalyst can be added with the compound ingredients, or further downstream in the mixer or can be added to the polymeric material after extrusion.
  • the invention is also based on the discovery that it is not necessary to pass the silane, free-radical activator and polymer through the entire length of an extruder in order to carry out the grafting reaction to the extent required to form a crosslinkable composition. It was also discovered that, in the method of the present invention, it is not necessary to use more than one extrusion, i.e., it is not necessary to extrude the polymer, silane and free-radical catalyst to form the grafted copolymer and then extrude the resulting grafted copolymer with a silanol condensation catalyst to form the crosslinkable composition.
  • the present invention is highly advantageous in permitting the conversion of existing extruders of the conventional type to the production of shaped crosslinkable polymer products and avoids the excessive expenses of purchasing, and installing specialized extruders and complex extruder controls as is the case with the one-step process.
  • the method of this invention produces a shaped, crosslinked, extruder, polymeric product by the steps comprising:
  • the apparatus used to carry out the method of this invention comprises an extruder having:
  • the invention is concerned with the crosslinking of polyethylene extrusions by the injection of a special silane formulation into molten polyethylene and by incorporating it into the molten polyethylene by using a mixing device retro-fitted to a conventional plastics extruder.
  • a preferred mixing device is known as a cavity transfer mixer US-A-4 419 014 which very rapidly incorporates the silane formulation so that uniform grafting of the silane onto the polyethylene takes place within the mixer.
  • the mixing device is easily fitted onto conventional extruders enabling extrusion companies to adapt existing extrusion lines to produce crosslinked polyethylene products, the grafted extrusions being crosslinked by exposure to water.
  • the products are principally pipes and cables but other products which benefit from higher service temperature capabilities; for example foam, film, profiles, sheets, beams, rods and the like, may also be made by this method of this invention.
  • the method of this invention is not confined to extrusions, e.g., cable insulation and pipe, but may be used also for blow moldings and injection moldings.
  • Polyethylene is well suited to the manufacture of cold water pipes.
  • the low heat distortion temperature of uncrosslinked polyethylene restricts its applications to low temperature uses.
  • Crosslinked polyethylene pipes can be used for hot water services; such applications being covered by DIN 16892 standard and Avis 14+15/81-100.
  • Crosslinked polyethylene pipes made by existing crosslinking processes are costly because:
  • This problem has been solved by the present invention by the injection of a silane formulation into a mixing device fitted between the extruder and die of a conventional polyethylene pipe extruder such that the silane formulation is very rapidly incorporated into the polymer melt and grafting of the silane to the polymer is achieved within the mixer.
  • the rapid incorporation and grafting can be satisfactorily achieved by using a cavity transfer mixer as described in US-A-4,419,014 fitted with an injector having a non-return valve for injecting the silane formulation.
  • the present invention enables the production of crosslinked polyethylene (XLPE) extrusions such as pipes for hot water applications on extrusion lines originally used or intended for the extrusion of non-crosslinked polyethylene. This had not been previously technically and economically feasible.
  • XLPE crosslinked polyethylene
  • the shaped product made according to the inventive process can be also cable insluation and sheathing, film, foam, profiles, rods, beams and sheets of increased temperature resistance as well as mechanical properties, physical properties, stress cracking resistance, and resistance to gas and moisture permeability in polymers such as polyethylene.
  • a mixer 18 is mounted on the downstream end of the extruder and comprises a stator 20 bolted to the barrel 10 and a rotor 22 fixed to the forwarding screw 12, as by screw threads (not shown), to rotate with the screw 12.
  • a die 24 is fixed to the downstream end of the mixer 18 by means of a clamp 26 or other suitable means and heating units 28 are provided around the stator 20 and die 24.
  • the mixer 18 can be of any conventional type and is here shown as a cavity transfer mixer of the type described in detail in US-A-4,149,014.
  • An injector 30 passes through the upstream wall of the mixer 18.
  • the outer end of the injector 30 is connected to a one-way valve 32 which is connected to a delivery system 34 for the compounding ingredients including the hydrolyzable, olefinically unsaturated silane, free radical generator and silanol condensation catalyst.
  • the delivery system as shown in Fig. 1 comprises a reservoir 36 containing the compounding ingredients, a pump 38 and tubing 40 connecting the outlet of the reservoir 36 to the inlet of the pump 38.
  • the reservoir 36 is provided with a suitable volumetric and gravimetric control (not shown). For laboratory trials burette is a convenient reservoir.
  • the outlet of the pump 38 is connected by tubing 42 through a T-connector 44 to the inlet of one-way valve 32.
  • the T-connector is also connected to a pressure transducer 46 which is connected to a recording instrument (not shown).
  • the space above the compounding ingredients in the reservoir 36 is vented through a dessicant-filled container 48 to the atmosphere.
  • the injector 30 connected to the one-way valve 32.
  • the injector 30 comprises a long tube 50 of sufficient length to pass completely through the wall of stator 20 and terminate very close to the rotor 22 such that the inner tip 52 of the injector is well below the surface of polymeric material flowing in the space between the rotor 22 and stator 20.
  • the inner surface of the tip 52 is formed on its inner end with a valve seat that mates with a valve head 54 disposed on the inner end of a long stem 56 that extends coaxially through said tube.
  • the outer end of the stem 56 is fixed to a slide 58, as-by screw threads (not shown) and a lock nut 60.
  • the slide 56 is slidably mounted in a chamber 62 and is adapted to slide between the forward wall 64 of the chamber 62 and its rearward wall 66.
  • a coil spring 68 is positioned coaxially with stem 56 and bears upon the slide 58 and forward wall 64 to bias the slide 58 and stem 56 outwardly and cause the valve head 54 to seat against the valve seat on tip 52.
  • valve head 54, valve stem 56 and slide 58 move to unseat the valve head from the seat on tip 52 and thereby open the valve and permit flow of fluid out of the tube 50 into the polymeric material occupying the space between the rotor 22 and stator 20.
  • the outer end of chamber 62 is connected to tubing 42 which is connected to pump 38 which delivers fluid compounding ingredients to the chamber 62. Bores 70 are provided through slide 58 to permit passage of fluid past the slide 58.
  • the mixer 18 can be of any conventional type and is shown in the drawings as a cavity transfer mixer described in detail in US-A-4,419,014, the disclosure of which is incorporated herein by reference.
  • Fig. 3 illustrates the arrangement of cavities 72 around the inner circumference of the stator 20 and the cavities 74 around the outer circumference of rotor 22.
  • the facing surfaces on the stator 20 and rotor 22 are formed with respective pluralities of semispherical cavities 72 and 74 respectively.
  • the cavities 74 on rotor 22 are disposed in a plurality of circumferentially extending rows.
  • the adjacent rows of cavities on the rotor are circumferentially displaced such that the center of each cavity 74 in a given row lies midway between the centers of the two nearest cavities 74' in each adjacent row.
  • circles 74a, 74b and 74c represent cavities in one row in the rotor
  • circles 74a', 74b' and 74c' represent cavities in the adjacent row on one side
  • 74a", 74b" and 74c" represent cavities in the adjacent row on the other side.
  • the cavities 72 on the stator 20 are disposed in a plurality of circumferentially extending rows, adjacent rows on the stator being displaced such that cavities 72 in a given row are offset by half the distance between the centers of the two nearest cavities 72' in each adjacent row.
  • Fig. 4 also illustrates the axial offset of the circumferential rows of cavities 72 on the stator 20 in relation to adjacent circumferential rows of cavities 74 on the rotor 22. More specifically, the circumferential line joining the centers of any given row of cavities 72 on the stator 20 lies midway between the two circumferential lines on either side of it joining the centers of cavities 74 on the rotor 22. The cavities 72 and 74 overlap such that molten polymer passing from the extruder barrel 10 to the die 24 is subjected to laminar shear within the cavities and cut and turned as it passes backwards and forwards between cavities on the rotor 22 and stator 20.
  • the injector 30 is so positioned that the tip 52 is located just upstream from the most upstream cavity or at the most upstream circumferential row of cavities 74 on the rotor 22.
  • the extruder is operated in a normal fashion by loading polymeric material, e.g. polyethylene pellets, into the hopper 8 where it is fed to the feed-transport zone 2 which delivers it to the compression and melting zone 4 where it is converted to a compacted melted polymeric material.
  • the compacted, melted polymeric material is delivered to the metering-pumping zone 6 and thence into the mixer 18.
  • Compounding ingredients are pumped, in appropriate amounts, from the reservoir 36 through the injector 30 into the compacted, melted polymeric material as it enters the mixer 18.
  • the compounding ingredients and compacted, melted polymeric material are rapidly and well mixed in the mixer 18.
  • residence time and temperature in the mixer 18 can be provided to generate free radical sites in the polymeric material and complete grafting of the silane onto the polymeric material to a sufficient extent to allow an adequate extent of crosslinking upon subsequent exposure to water. It was also surprising to find that mixing of the molten polyethylene and the compounding ingredients can be achieved adequately in the relatively short mixer to provide relatively uniform mixing and no troublesome formation of small gels.
  • the grafted polyethylene then travels through the die 24 and through cooling and haul-off systems as normally used for polyethylene extrusion. The extrusion is then exposed to hot water or moist conditions in known ways until the grafted polymer is adequately crosslinked.
  • the rotational speed of the forwarding screw 12 can be varied over a wide range, e.g., from 30 to 105 rpm for a 38 mm diameter forwarding screw.
  • the temperature in each of the three zones can be varied over wide ranges and basically depends upon the melting characteristics of the polymeric material being extruded.
  • the temperature of polyethylene in the feed-transport zone 2 can range from 100°C to 145°C
  • the temperature of the material in the compression-melt zone 4 should be higher than the temperature of the material entering said zone and of course above the melting point of the polyethylene, and can range from 135°C to 155°C.
  • the temperature of the polyethylene in the metering-pumping zone 6 is higher than the temperature of the material entering said zone and can range from 145°C to 180°C.
  • Representative temperatures of the polyethylene in the mixer 18 can be varied over a wide range of 145°C to over 210°C, typically being, of course, higher than the temperature of the material entering the mixer. These temperatures are based on readings taken from controller thermocouples (not shown) fitted into the metal of the extruder barrel 10 but the polymer melt temperature could be higher as a result of mechanically produced heat.
  • the temperature of the polyethylene leaving the die 24 need not exceed the temperature of polyethylene entering the die, and representatively range from 155°C to 250°C.
  • the output rate depends largely on the type and size of extruder used and, for a 38 mm diameter extruder operating at a screw speed in the above-mentioned range, can range from 25 g/min to 350 g/min.
  • the proportion of hydrolyzable, olefinically unsaturated silane based on the weight of polymeric material also is not narrowly critical and can range from 0.1 to 10 wt.%, preferably 0.7 to 3 wt. %, of silane based on the total weight of polymeric material.
  • the amounts of free radical generator also is not narrowly critical and can be varied over wide ranges, for example, from 0.01 wt.% to 0.3 wt.%, preferably 0.05 to 0.2 wt.%, based on the total weight of polymeric material.
  • the proportion of silanol condensation catalyst is not narrowly critical, illustratively ranging from 0.01 to 0.2 wt.%, preferably 0.02 to 0.08 wt.%, based on the total weight of polymeric material.
  • Polymers to be used in the process according to the present invention include the polymers of alpha-olefins having 2 to 6 carbon atoms such as ethylene, propylene, 1-butene; 1-pentene; 1-hexene; isobutylene; 2-methyl-1-butene; 3-methyl-1-butene; 2,2-dimethylpropene; 2-methyl-1-pentene; 3-methyl-1-pentene; 4-methyl-1-pentene; 2,2-dimethyl-1-butene; 2,3-dimethyl-1-butene; 3,3-dimethyl-1-butene; and 2-ethyl-1-butene.
  • alpha-olefins having 2 to 6 carbon atoms such as ethylene, propylene, 1-butene; 1-pentene; 1-hexene; isobutylene; 2-methyl-1-butene; 3-methyl-1-butene; 2,2-dimethylpropene; 2-methyl-1-pentene; 3-methyl-1-pentene; 4-methyl-1
  • the olefin polymer reactant employed in the invention is either a homopolymer of an alpha-olefin having 2 to 6 carbon atoms or a copolymer of two alpha-olefins, e.g., copolymers of ethylene and propylene.
  • Modified poly-alpha-olefins such as chlorinated polyethylene can be made in this invention. Any polymer that is capable of being extruded and is capable of being crosslinked by a hydrolyzable olefinically unsaturated silane is suitable for use in this invention.
  • any polymer or copolymer chemically suitable for silane crosslinking can be used, or blends of such polymers.
  • examples are ethylene-vinyl acetate copolymers, polyamides and ethylene-propylene rubbers.
  • Hydrolyzable olefinically unsaturated silanes suitable for grafting onto and crosslinking the polymers according to this invention include organofunctional silanes of the general formula: wherein R represents a monovalent olefinically unsaturated hydrocarbon or olefinically unsaturated hydrocarbonoxy group which is reactive with the free radical sites generated in the polymer by the free radical generator, R 1 represents a hydrolysable organic group such as an alkoxy group having 1 to 12 carbon atoms (e.g. methoxy, ethoxy, butoxy), aralkoxy groups (e.g. phenoxy), aliphatic acyloxy groups having 1 to 12 carbon atoms, (e.g.
  • X represents a monovalent alkyl, aryl or aralkyl group (e.g. ethyl, methyl, propyl, phenyl, benzyl), m is 0 or 1 and n is 0, 1 or 2.
  • unsaturated silanes are vinylmethyldimethoxysilane, vinyltriethoxysilane, vinyltrimethoxysilane, allyltriethoxysilane, allyl- methyldiethoxysilane, allytriethoxysilane, diallyldimethoxysilane, allylphenyldiethoxysilane, methoxy- vinyldiphenylsilane, dodecenylvinyldipropoxysilane, didecenyldimethoxysilane, didodecenyldimethoxy- silane, cyclohexenyltrimethoxysilane, hexenylhexoxydimethoxysilane, vinyl - tri - n - butoxysilane, hexenyltri - n - butoxysilane, allyldipentoxysilane, butenyldodecoxysilane, dec
  • the silanes will contain two or three hydrolysable organic groups and a vinyl or allyl group as the group reacting with the free radical sites formed in the polymer by the free radical generator.
  • the free radical generating compound there may be used any compound which is capable of producing free radical sites in the polymer, the reaction conditions depending on temperature and retention time in the CTM needed for achieving a suitable half life time.
  • the preferred free-radical initiators are organic peroxides and peresters such as tert. - butylperoxyneodecanoate, tert. - butylperoxy- neohexanoate, tert. - amylperoxypivalate, tert.
  • butylperoxypivalate bis (3,5,5 - trimethyIhexanoyI) peroxide, bis (2 - methylbenzoyl) peroxide, di - decanoylperoxide, di - octanoylperoxide, di - lauroyl- peroxide, tert. - butylperoxy - 2 - ethylhexanoate, tert. - butylperoxy diathylyacetate, tert. - butylperoxy- butyrate, 1,1-di. tert. - butylperoxy - 3,5,5 - trimethylcyclohexane, 1,1 - di.
  • butylperoxide 2,2 - azo bis (2,4 - dimethylvaleronitrile), azo - bisisobutyronitrile, di - benzoylperoxide, 2,5 - dimethyl - 2,5 - bis (tert. - butylperoxy) hexane, tert. butyl peroctoate, tert. butyl perbenzoate and tert. butylcumylperoxide as well as combinations thereof.
  • Silanol condensation catalysts used for the crosslinking of the polymer under the influence of water molecules are metal carboxylates, such as for example: dibutyltindilaurate, dioctyltin dilaurate, stannous acetate, stannous octoate, dibutyltin dioctoate, di-octyl tin-bis (isooctylmaleate), di - octyl-tin-bis (isooctylthioglycolate) as well as organometal compounds such as the titanium esters and chelates, for example, tetrabutyl titanate, tetranonyl titanate, and bis (acetylacetonyl) di-isopropyl titanate, organic bases, such as, ethylamine, hexylamine, dibutylamine, and piperidine, and acids, such as, fatty acids and mineral acids.
  • metal carboxylates such
  • Further additives which can be incorporated into the hot polymer melt through the injector into the mixing head are any of the antioxidants and heat stabilizers commonly used in the processing of polyolefines and combinations thereof.
  • minerals for improving flame retardancy or as an internal source of water for the crosslinking e.g. aluminum trihydrate, zeolite or carbon blacker minerals like chalk, talc, mica, silica and silicates can be injected into the polymer as it enters the mixing head or CTM.
  • the silanes and other additives can be metered into the mixing head or CTM separately or preferably, as a more efficient way, as pre-manufactured binary, ternary, or quaternary formulations.
  • Such formulations contain the silane and condensation catalyst or free radical initiators or inhibitors or stabilizers or combinations thereof.
  • the silanes alone or as binary, ternary, quaternary formulations with the free radical initiators, condensation catalysts, antioxidants, etc. can be used for the pre-treatment of the above-mentioned minerals (aluminum trihydrate, zeolite or silica). These pre-treated fillers can be then more easily incorporated into the hot-melt through the CTM mixing head.
  • the system of this invention can be modified to allow the incorporation of other additives, both liquids and solids, injected either with the silane mixture, by a separate pump or through a separate open port.
  • the mixer can be extended with a CTM configuration, or alternative mixing device, for example, a pinned mixer, a screw, or a static mixer.
  • the products can be manufactured pursuant to this invention using a molten polymer pumping process and the mixer can be driven by the polymer pumping screw or it can be driven separately.
  • Twin screw extruders can also be used with these various configurations.
  • the extruder used in each example is illustrated in Fig. 1 and is a Bone Bros. single screw extruder having a barrel diameter of 1.5" (38 mm), a screw length of 36" (915 mm), a screw LID of 24:1, a feed-transport zone length of 8D (12", 305 mm), compression-metering zone length of 8D (12", 305 mm), a metering-pumping zone length of 8D (12", 305mm), a channel depth in the feed-transport zone of 0.248" (6.3 mm), a channel depth in the metering-pumping zone of 0.083" (2.1 mm), a nominul compression ratio (depth ratio) of 3:1, a pitch of 1D and a 5.52 kW (7.5. horsepower), variable speed AC commutator motor.
  • the extruder barrel is provided in the three zones with 3 term temperature controllers operating electrical resistance heating and proportional cooling for each of the three zones.
  • the mixer employed in the examples is diagrammatically shown in the drawings and described in US-A-4,419,014.
  • Each of the stator and rotor used has seven circumferential rows with five cavities in each row.
  • the mixer used has a nominal diameter of about 1.5 inch (38 mm) and a nominal LID ratio of 4: 1.
  • an 8 mm diameter strand die having a streamlined entry was used.
  • the compounding ingredients were injected through the non-return valve 32 and injector 30 shown in Figs. 1 and 2 and the tip 52 of the injector was positioned below the surface of the melt flowing into the mixer.
  • a Bran and Lubbe pump was used to pump the compounding ingredients through the one-way valve and injector.
  • crosslinking formulation referred to as "XL Form.” in the examples, and contained 89 wt.% vinyltrimethoxysilane, 8 wt.% dicumylperoxide and 3 wt.% dibutyltin dilaurate.
  • the general extrusion conditions described in the examples refer to metal temperatures of the barrel at B1, B2 and B3. These temperatures were measured at the midpoint of each of the feed-transport zone 2, compression-melting zone 4 and metering-pumping zone 6, respectively.
  • the temperature given for the CTM i.e., the cavity transfer mixer, is a metal temperature measured at the midpoint of the CTM.
  • the die temperature is a metal temperature measured at the midpoint of the die.
  • the pump pressure given is the pressure generated by pump 38 in the crosslinking formulation being pumped through tubing 42, one-way valve 32 and injector 30.
  • samples of the extrudate from the die and samples of extrudate taken from three bleed ports 1, 2 and 3 located at, respectively, the second, fourth and sixth circumferential rows of cavities were tested for crosslink density by xylene extraction.
  • shavings of the extrudate were taken, weighed and placed in 100 ml of xylene which was boiled for seven hours after which the resulting mineral was vacuum filtered onto preweighed filter paper to recover all of the residue remaining undissolved in the xylene.
  • the residue represents the crosslinked portion of. the extrudate and the dissolved portion represents the uncrosslinked portion.
  • the weight percent of insoluble material, i.e., crosslinked polymer, in the extrudate is calculated by dividing the weight amount of residue by the weight amount of initial sample placed into the xylene and multiplying by 100.
  • Residue (dry) G (%) provides the hot xylene extraction test results on samples of extrudate that were measured and immediately stored in a desiccator to avoid any contact with moisture; the G standing for grafted composition and implying little or no crosslinking because of the avoidance of any contact with moisture.
  • the designation "Residue (wet) XL (%)” refers to the hot xylene test results performed on samples of the extrudate that were simply stored in a polyethylene bag until testing and which, prior to testing, were boiled in water for four hours to crosslink the grafted polymeric material prior to subjecting it to hot xylene extraction.
  • the dumb-bell specimens are then subjected to a hot deformation test pursant to IEC 502,1983 to determine the maximum extension under load and permanent extension of the sample.
  • each test piece is suspended at one end by a grip in an oven and a lower grip is attached to the lower end of each test piece for the purpose of suspending weights therefrom.
  • a load of 20 N/cm 2 was applied to the test piece for 15 minutes while suspended in the oven at a temperature of 200°C.
  • the load of 20N/cm 2 is based on the cross-sectional area of the neck of the dumb-bell shaped test pieces.
  • the test pieces are initially formed with spaced marker lines extending in parallel, transversely across the narrow parallel portion or neck. The initial, pretest distance separating the marker lines is 20 mm before exposure to load and elevated temperature.
  • the distance between the marker lines is measured and the increase in distance over the initial pretest distance is divided by the initial pretest distance and multiplied by 100 to give the percent extension at 200°C which is reported as "Exten. at 200°C (%)" in the tables of the examples.
  • a lower percent extension at 200°C indicates a higher degree of crosslinking and a greater percent extension indicates a lower degree of crosslinking.
  • the load is then removed and the test pieces are allowed to recover for 5 minutes at 200°C. They then are removed from the oven and allowed to cool slowly to ambient temperature after which the distance between the marker lines is measured, from which distance the initial (pretest) distance between the marker lines is subtracted to give the mm of permanent extension imparted to the test piece.
  • the mm of permanent extension is then divided by the initial distance between the marker lines and multiplied by 100 to give the percent permanent extension, and is reported as such in the tables. The lower the percentage of permanent extension generally indicates a higher level of crosslinking. For XLPE insulation and sheating applications, the maximum elongation tolerable is 175% and the maximum permanent elongation tolerable is 15% according to present practices.
  • the extruder was started and medium density polyethylene (Vestolen-A4516) having a melt flow index (ISO/R1133 190/2 procedure 4) of 7 g/10 min and iSO/R1133 190/5 procedure 5) of 20 g/10 min was fed to the hopper of the extruder.
  • the density (lSO/R1183) of the polyethylene was 0.945 g/cm 3 .
  • the screw speed as given in Table 1 below was set and the B1, B2, B3, CTM and die temperatures were measured and are listed in Table 1 which also provides the motor current and pump pressure for each of the screw speeds specified.
  • the extruder output rate at each screw speed also was measured by cutting and weighing samples at 1 min intervals and the output rate determined by this method for each screw speed is listed.
  • Injection of the XL Formulation was then started with the pump 38 adjusted to provide the desired concentration of XL Formulation in the polymeric material given in Tables 2, 3 and 4 below.
  • the output rate was measured again and the injection pump 38 was adjusted as necessary in order to correlate the concentration of XL Formulation injected to any changes in the output rate of polyethylene being fed to the mixer 18 by the extruder.
  • Tables 2 and 3 show that more than 50% and as high as 80% of each of the polymeric extrudate was crosslinkable and that the resulting crosslinked extrudates are acceptable for insulation and sheathing applications.
  • Table 4 show a steady increase in grafting as the polymeric material progressed through the mixer and the degree of grafting just before the polymeric material left the mixer was sufficiently high to provide 65% or more crosslinked polymer.
  • Example 1 The procedure of Example 1 was carried out except that instead of the polyethylene identified therein as Vestolen A4516, a different polyethylene, namely, Unifos DFDS4444, having a melt flow index (ASTM D1238) of 2.2 g/10 min and a density (ASTM D1928C) of 922 kg/m 3 was used.
  • the general extrusion conditions are given in Table 5 and the test results are given in Tables 6, 7 and 8.
  • results given in Tables 6 and 7 show that 60% or more, as high as 82%, of the polymeric material is crosslinkable and that the resulting crosslinked extrudates are acceptable for insulation and sheathing applications.
  • results of Table 8 illustrate a steady increase in the crosslinkability, i.e., in the degree of grafting, as the polymeric material passes through the mixer.
  • Example 1 The procedure given in Example 1 was used except that in place of Vestolen A4516 polyethylene, there was used a polyethylene identified as Unifos NEWS8019, and LLDPE which has more potentially reactive sites than other polyethylenes, having a melt flow index (ASTM D1238) of 4 g/10 min and a density (ASTM D1928C) of 934 kg/m 3 .
  • the general extrusion conditions are given in Table 9 and Tables 10-13 provide the results at the indicated screw speeds and XL formulation concentrations.
  • Table 10 illustrates the increase in crosslinkability of polymeric extrudate as the proportion of crosslinking formulation (i.e., silane, free radical generator and silanol condensation catalyst) are increased and a crosslinkability of as much as 89 wt. % of the polymeric material is attainable and that crosslinked extrudates which have excellent hot extension properties can be made.
  • Table 11 illustrates polymeric extrudates which are at least 61% crosslinkable and as much as 89% crosslinkable.
  • Tables 12 and 13 illustrate the excellent hot extension properties of the polymeric extrudates identified therein.
  • Example 1 The procedure of Example 1 was carried out except that instead of the polyethylene described therein there was instead used a polyethylene identified as Hoechst GF 7740F2 having a melt flow index (ASTM D 1238) of 0.5 g/min and a density (ASTM D1928C) of 942 kg/m 3 .
  • a polyethylene identified as Hoechst GF 7740F2 having a melt flow index (ASTM D 1238) of 0.5 g/min and a density (ASTM D1928C) of 942 kg/m 3 .

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Claims (8)

1. Procédé d'obtention d'un produit polymérique réticulé extrudé, façonné, consistant:
(a) à introduire un polymère thermoplastique dans la zone d'alimentation d'une extrudeuse munie d'une vis de transport et d'un cylindre dans lequel la vis est placée et tourne pour faire avancer le polymère à travers le cylindre;
(b) à tasser et faire fondre le polymère dans ledit cylindre;
(c) à faire passer le polymère tassé, fondu, résultant à travers un mélangeur d'extrusion (18) placé à l'extrémité de décharge de l'extrudeuse, le mélangeur étant muni d'un stator creux (20) aligné dans l'axe de l'extrémité de décharge du cylindre (10) et destiné à recueillir le polymère tassé, fondu, en provenant, et d'un rotor (22) placé dans le stator, aligné dans l'axe de la vis (12) et pouvant tourner ainsi à l'intérieur du stator, les surfaces du rotor et du stator présentant des éléments de mélange destinés à soumettre le polymère tassé, fondu, passant à travers le mélangeur à une action de mélange par fort cisaillement;
(d) à injecter des quantités proportionnelles d'ingrédients de mélange, comprenant un agent engendrant des radicaux libres, dans le polymère tassé, fondu;
(e) à mélanger les ingrédients de mélange et le polymère tassé, fondu, dans le mélangeur;
(f) à extruder le mélange résultant hors du mélangeur (18) à travers une filière d'extrusion (24) pour former le produit façonné; et
(g) à soumettre l'extrudat de l'étape (f) à l'action de H20 en présence d'un catalyseur de condensation de silanol jusqu'à réticulation du polymère,

caractérisé en ce que les éléments de mélange utilisés dans l'étape (c)-connus en eux-mêmes- comprennent plusieurs rangées de cavités concaves (72; 74) disposées à la périphérie du stator et du rotor, les rangées étant séparées axialement de sorte que les rangées sur le stator présentent un décalage axial par rapport aux rangées sur le rotor et qu'il existe un chevauchement axial des cavités dans des rangées adjacentes sur le stator et le rotor, les cavités (72) dans des rangées adjacentes sur le stator présentant un décalage circonférentiel et les cavités (74) dans des rangées adjacentes sur le rotor présentant un décalage circonférentiel; et en ce que, pour la réticulation du polymère thermoplastique, un silane hydrolysable à insaturation oléfinique est injecté dans le polymère tassé, fondu, puis une étape de mélange (e) est mise en oeuvre jusqu'au greffage du silane sur le polymère.
2. Procédé suivant la revendication 1, dans lequel est utilisé un silane à fonctionnalité organique répondant à la formule générale:
Figure imgb0018
dans laquelle R représente un groupe hydrocarboné ou hydrocarbonoxy monovalent à insaturation oléfinique qui est réactif avec les sites de radicaux libres engendrés dans le polymère par l'agent engendrant des radicaux libres, R1 représente un groupe organique hydrolysable, X représente un groupe alkyle, aryle ou aralkyle monovalent, m a la valeur 0 ou 1 et n a la valeur 0, 1 ou 2.
3. Procédé suivant la revendication 2, dans lequel le silane est le vinyltriméthoxysilane.
4. Procédé suivant les revendications 1 à 3, dans lequel l'agent engendrant des radicaux libres est un peroxyde organique, de préférence le peroxyde de dicumyle.
5. Procédé suivant les revendications 1 à 4, dans lequel les ingrédients de mélange comprennent le catalyseur de condensation de silanol.
6. Procédé suivant la revendication 5, dans lequel le catalyseur de condensation est le dilaurate de dibutylétain.
7. Procédé suivant les revendications 1 à 3, dans lequel le polymère est le polyéthylène.
8. Procédé suivant les revendications 1 à 7, dans lequel les ingrédients de mélange comprennent le vinyltriméthoxysilane, le peroxyde de dicumyle et le dilaurate de dibutylétain.
EP85104444A 1984-04-13 1985-04-12 Procédé pour l'extrusion en une seule phase de produits extrudés en matière polymérique réticulés Expired EP0163865B1 (fr)

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Also Published As

Publication number Publication date
WO1985004618A1 (fr) 1985-10-24
EP0163865A1 (fr) 1985-12-11
GR850907B (fr) 1985-11-25
DK158500B (da) 1990-05-28
CA1263512A (fr) 1989-12-05
PT80277A (en) 1985-05-01
FI83488B (fi) 1991-04-15
DK158500C (da) 1990-10-29
ES542191A0 (es) 1987-06-01
ES8701025A1 (es) 1986-11-16
MX166259B (es) 1992-12-24
DK576185D0 (da) 1985-12-12
FI854961A0 (fi) 1985-12-13
DK576185A (da) 1985-12-12
ES551525A0 (es) 1986-11-16
PT80277B (en) 1988-05-03
JPH0455850B2 (fr) 1992-09-04
DE3563322D1 (en) 1988-07-21
US4857250A (en) 1989-08-15
BR8506603A (pt) 1986-04-15
FI83488C (fi) 1991-07-25
ES8706064A1 (es) 1987-06-01
AU590513B2 (en) 1989-11-09
FI854961A (fi) 1985-12-13
KR860700016A (ko) 1986-01-31
JPS61501973A (ja) 1986-09-11
AU4232885A (en) 1985-11-01
KR920007727B1 (ko) 1992-09-16

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